EP0710799B1 - Procédé d'oxydation thermiques de liquides résiduaires - Google Patents

Procédé d'oxydation thermiques de liquides résiduaires Download PDF

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Publication number
EP0710799B1
EP0710799B1 EP95116792A EP95116792A EP0710799B1 EP 0710799 B1 EP0710799 B1 EP 0710799B1 EP 95116792 A EP95116792 A EP 95116792A EP 95116792 A EP95116792 A EP 95116792A EP 0710799 B1 EP0710799 B1 EP 0710799B1
Authority
EP
European Patent Office
Prior art keywords
liquid
flue gas
fan
stream
liquid waste
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP95116792A
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German (de)
English (en)
Other versions
EP0710799A2 (fr
EP0710799A3 (fr
Inventor
Uwe Listner
Martin Schweitzer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bayer AG
Original Assignee
Bayer AG
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Filing date
Publication date
Application filed by Bayer AG filed Critical Bayer AG
Publication of EP0710799A2 publication Critical patent/EP0710799A2/fr
Publication of EP0710799A3 publication Critical patent/EP0710799A3/fr
Application granted granted Critical
Publication of EP0710799B1 publication Critical patent/EP0710799B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/008—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for liquid waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/12—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating using gaseous or liquid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/442—Waste feed arrangements
    • F23G5/446—Waste feed arrangements for liquid waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/12—Sludge, slurries or mixtures of liquids

Definitions

  • the invention relates to a method for the complete thermal oxidation of liquid waste.
  • the waste material is then transferred to a hot flue gas stream introduced, evaporated and thermally oxidized.
  • the flue gas flow must be closed for this purpose contain the oxygen necessary for the oxidation.
  • An essential step is the utilization of the thermal Energy from a flue gas stream coming from an incinerator for thermal oxidation and thus disposal of liquid waste.
  • the oxygen required for this oxidation process is called hot Flue gas stream delivered; i.e. the flue gas flow must be sufficient Contain oxygen.
  • the hot flue gas e.g. through a waste incineration plant generated, must be burned with an excess of oxygen be worked so that part of the unused oxygen with the hot flue gas is discharged.
  • this is an incineration plant with a Afterburning chamber, which is supplied with the liquid waste to be disposed of become.
  • a Afterburning chamber which is supplied with the liquid waste to be disposed of become.
  • one or installed several special burners which applied the liquid waste fuel become.
  • the liquid waste fuel is in the burner flame atomized finely.
  • the swarm of drops generated forms a full cone.
  • Each Burner is also used in sufficient quantities of combustion air Atomization of the liquid waste material required compressed air.
  • the atomized liquid is initially available as a droplet collective that mixes with the Initial velocity of the atomization is moved into the combustion chamber. Between the single drop flows out of the nozzle at the speed of sound Atomizing air. This two-phase mixture is initially relatively cold Combustion air enveloped.
  • the invention has for its object also poorly combustible liquid waste fuels to be introduced into the afterburning chamber in such a way that even with unfavorable ones Burning conditions a complete burnout is guaranteed.
  • this object is achieved according to the invention in that the liquid waste fuel is injected into the hot flue gas stream with a flow component perpendicular to the main flow direction as a fan-shaped flat jet using one or more two-substance nozzles, which pulsate at a frequency of 5 s -1 to 70 s -1 , preferably 10 s -1 to 20 s -1 are operated, a fan-shaped spray carpet with relatively coarse drops of long range and a flat spray carpet with relatively fine drops of short range being generated in alternation at each two-component nozzle, so that the flue gas stream alternating with finely sprayed drops of short range and coarse that flue gas with a relatively large throw penetrating drops.
  • the liquid waste material is preferably injected into a flue gas stream whose temperature is at least 800 ° C and its oxygen content at least is so high that complete oxidation of the combustible materials is guaranteed is.
  • the geometry of the two-component nozzles and the flow conditions (throughput and Operating pressures) are chosen so that the opening angle of the fan-shaped Spray carpets is 60 ° to 160 °.
  • the atomizing gas throughput and the liquid throughput at the two-fluid nozzles is adjusted so that the time average flow ratio of air and liquid flows at each Two-component nozzle is in the range of 0.01 to 0.2, while the instantaneous value of the Flow ratio fluctuates according to the pulsation frequency.
  • the pulsating mode of operation can be caused by periodic exposure to the Two-substance nozzle with compressed gas or liquid. Alternatively, the pulsating operation even when compressed air and Fluid generated in the two-fluid nozzle itself.
  • Fig. 1 is a main combustion chamber 1 with a burner 2 and a main flame 3 shown.
  • the main flame 3 becomes so much combustion air or oxygen that the flowing out of the main combustion chamber 1
  • Flue gas 4 still has a considerable residual oxygen content (more than 6%).
  • the Oxygen content of the flue gas can be varied by the main flame 3 more or less in excess oxygen or combustion air supplied becomes
  • the oxygen-containing flue gas 4 leaves the main combustion chamber 1 with a Temperature from 1000 ° C to 1400 ° C and then flows into the afterburner 5. Liquid is injected into the afterburning chamber 5 Waste fuels, which are then in the hot flue gas stream with the residual oxygen are thermally oxidized and thus disposed of Technology), one or more burners are installed in the afterburning chamber are equipped with their own burner air supply. The ones to be treated liquid waste is injected directly into the flames of these burners.
  • the new process eliminates the need for burners in the afterburner.
  • the liquids to be oxidized are made with the help of special Two-substance nozzle lances 6 are injected into the flue gas stream in a fan shape.
  • the fan-shaped Spray carpet 7 is shown in Fig. 2. Its transverse extent is b much larger than its thickness a (see Fig. 1).
  • the main difference compared to conventional nozzle lances is that the used here Two-fluid nozzle lances 6 alternate with a fan-shaped spray carpet relatively coarse drops with a long range and a fan-shaped spray carpet generate with relatively fine drops of small range, so that the flue gas flow 4 alternating with finely sprayed drops of short range and rough that Flue gas with a relatively large throw penetrating drops becomes.
  • This pulsating operation is hereinafter referred to as "bimodal operation" designated.
  • bimodal two-substance nozzle lances 6 are arranged in the afterburning chamber 5 in a rotationally symmetrical manner.
  • the fan-shaped spray carpets 7 of the two-substance nozzle lances 6 partially overlap.
  • the atomizing gas for example air and the liquid to be disposed of, is fed to a bimodal two-substance nozzle lance 6.
  • the opening angle of the fan-shaped spray carpets is approx. 120 °.
  • the spray level is perpendicular to the main direction of flow of the hot flue gases. However, this condition need not be strictly observed. In the bimodal mode of operation, coarse and fine drops of different speeds and thus throwing distances replace each other.
  • Bimodal spraying is also characterized by a very wide range of drops. At a throughput of 1.5 m 3 / h, coarse drops with a diameter of approx. 2 mm and a range of approx. 6 m were observed on the one hand and small drops of approx. 30 ⁇ m with a range of approx. 0.4 m on the other.
  • An essential characteristic of this mode of operation is the rapid change in time between fine drops and coarse drops. The fine drops are generated when the two-substance nozzle lance works in the two-substance atomization mode. The coarse drops, on the other hand, arise in the subsequent mode of the pressure nozzle operation.
  • the fine drops evaporate quickly and ignite quickly in the hot atmosphere. This results in a flame that stabilizes itself near the nozzle.
  • the turbulence bales 8 formed on contact with the flue gas and formed from steam and flue gas are considerably smaller than in the usual post-combustion because neither significant drop collectives nor cold combustion air hinder the evaporation of the liquid and also do not delay the mixing with the hot flue gas.
  • a steam trail with spatially different flue gas / steam mixture ratios is generated along their trajectory, the quantity ratio of steam to oxygen-containing flue gas becoming smaller over time. If there is a combustible mixture locally, a stable combustion takes place after an ignition delay time in the ms range.
  • the pulsation nozzle forms the front part of the one shown in FIGS. 1 to 3 4 and consists of a in a welding sleeve 9th screwed-in commercially available flat jet nozzle 10, one with the welding sleeve 9 firmly connected cladding tube 11, one axially displaceable in the cladding tube Inner tube 12, and a liquid distributor 13 attached to the inner tube.
  • the inner tube 12 with the liquid distributor 13 attached is via centering webs 14 axially displaceably mounted in the cladding tube 11.
  • the required seal of the slidable inner tube 12 relative to the cladding tube 9 is not shown here.
  • the liquid to be oxidized flows through the inner tube 12 and through the Annular gap 15 between the inner tube 12 and the cladding tube 11 as compressed air gaseous atomizing medium
  • the liquid distributor 13 consists of a frontally sealed, placed on the inner tube 12 pipe piece with Exit bores 16 oriented perpendicular to the axis and offset from one another.
  • the liquid to be oxidized exits the inner tube 12 through the outlet bores 16 into a first resonance chamber adjoining the distributor 13 17 a while the compressed air through the annular gap between the inner tube 12th and cladding tube 11 is supplied.
  • the compressed air flows through the groove-like Open spaces 18 between the centering webs 14.
  • the outlet bores 16 are in the Distributor 13 attached so that they are each in the axial extension of the annular gap cross section partially closing centering webs 14; i.e. the exit holes 16 are in the dead space or in the flow shadow behind the Centering webs 14. In this way, a mixing of the liquid phase and the gaseous phase (compressed air) in the resonance chamber 17 largely excluded.
  • the resonance chamber 17 is on the long side through the cladding tube 11, on the front side Entry through the liquid distributor 13 and at the outlet through a throttle or Aperture 19 with an inner diameter of the resonance chamber 17 greatly reduced cross-section limited. If the inner tube moves 12 in the cladding tube 11 changes the effective length a and thus also the volume the resonance chamber 17.
  • Another resonance chamber 20 connects to the throttle 19. Through the actual nozzle opening on the nozzle head, which here as a narrow rectangular Slit 21 is formed, occurs in the second resonance chamber 20 a two-phase mixture of compressed air / waste liquid into the flue gas duct.
  • the second resonance chamber 20 can therefore also be regarded as a spray chamber become.
  • more than two resonance chambers could also be used can be connected in series, each with orifices or chokes are separated from each other.
  • the mass flow ratio tends K from an upper limit - this corresponds to a high proportion of gaseous atomizing medium all through the nozzle slot 21 flowing mass - to a lower limit value, in order to then return to the To increase the maximum value.
  • the upper limit corresponds to the state of the Fine atomization with a short range and the lower limit of education of coarse drops with a long range. This process is repeated periodically.
  • the repetition frequency or pulsation frequency can be increased or reducing the volume of the resonance chamber 17 to be changed. If the volume is e.g. by increasing the distance a increases, the frequency decreases (lower field in Fig. 5), while as the volume decreases, the pulsation frequency increases (upper Partial image in FIG.
  • the pulsation mode arises with the resonance chamber two-substance nozzle described above by itself (autopulsation). Instead of the auto pulsation mode Forced pulsation can also be induced if one Compressed air or liquid is periodically applied to the two-substance nozzle. This can e.g. done by so-called flutter valves, which are in the supply lines for the Compressed air or the liquid are installed.

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)
  • Chimneys And Flues (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Treating Waste Gases (AREA)

Claims (6)

  1. Procédé d'oxydation thermique complète de déchets liquides, dans lequel la matière du déchet est vaporisée et oxydée dans un écoulement (4) de gaz de fumée chauds qui contient également l'air nécessaire à l'oxydation, caractérisé en ce que le déchet combustible liquide est injecté dans l'écoulement (4) de gaz de fumée chaud avec une composante perpendiculaire à la direction principale d'écoulement, sous la forme d'un jet plat en entonnoir, à l'aide d'un ou plusieurs gicleurs (6) à deux matières qui travaillent de manière pulsée à une fréquence de 5 s-1 à 70 s-1, de préférence de 10 s-1 à 20 s-1, et sur chaque gicleur à deux matières (6), on crée en alternance un tapis de pulvérisation en forme d'éventail contenant des gouttes relativement grossières de grande portée et un tapis de pulvérisation (7) en forme d'éventail contenant des gouttes relativement fines à courte portée, de telle sorte que l'écoulement (4) de gaz de fumée reçoit en alternance de fines gouttes pulvérisées à courte portée et de grosses gouttes qui traversent le gaz de fumée à une portée d'expulsion relativement grande.
  2. Procédé selon la revendication 1, caractérisé en ce que le déchet liquide est injecté dans un écoulement (4) de gaz de fumée dont la température vaut au moins 800° C et dont la teneur en oxygène est au moins assez élevée pour assurer une oxydation complète des matières combustibles.
  3. Procédé selon les revendications 1 à 2, caractérisé en ce que l'angle d'ouverture du tapis de pulvérisation (7) en forme d'éventail est compris entre 60° et 160°.
  4. Procédé selon les revendications 1 à 3, caractérisé en ce que les débits de gaz de pulvérisation et de liquide sont réglés de telle sorte que la valeur moyenne dans le temps du rapport des débits massiques d'air et de liquide soit comprise dans la zone de 0,01 à 0,2 sur chaque gicleur (6) à deux matières, tandis que la valeur momentanée du rapport des débits massiques varie en fonction de la fréquence de pulsation.
  5. Procédé selon les revendications 1 à 4, caractérisé en ce que le fonctionnement pulsé est obtenu par une alimentation périodique du gicleur (6) à deux matières en gaz sous pression ou en liquide.
  6. Procédé selon les revendications 1 à 4, caractérisé en ce que le fonctionnement pulsé est créé de lui-même par la technique d'écoulement dans le gicleur (6) à deux matières, avec une alimentation constante dans le temps en gaz comprimé et en liquide.
EP95116792A 1994-11-07 1995-10-25 Procédé d'oxydation thermiques de liquides résiduaires Expired - Lifetime EP0710799B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4439670 1994-11-07
DE4439670A DE4439670A1 (de) 1994-11-07 1994-11-07 Verfahren zur thermischen Oxidation von flüssigen Abfallstoffen

Publications (3)

Publication Number Publication Date
EP0710799A2 EP0710799A2 (fr) 1996-05-08
EP0710799A3 EP0710799A3 (fr) 1998-01-14
EP0710799B1 true EP0710799B1 (fr) 2001-02-28

Family

ID=6532642

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95116792A Expired - Lifetime EP0710799B1 (fr) 1994-11-07 1995-10-25 Procédé d'oxydation thermiques de liquides résiduaires

Country Status (5)

Country Link
US (1) US5634413A (fr)
EP (1) EP0710799B1 (fr)
JP (1) JPH08210619A (fr)
CA (1) CA2162080A1 (fr)
DE (2) DE4439670A1 (fr)

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JPH11218316A (ja) 1998-02-03 1999-08-10 Risou Burner Kk 廃液焼却炉及び焼却方法
US20030022207A1 (en) * 1998-10-16 2003-01-30 Solexa, Ltd. Arrayed polynucleotides and their use in genome analysis
US20040106110A1 (en) * 1998-07-30 2004-06-03 Solexa, Ltd. Preparation of polynucleotide arrays
US6787308B2 (en) * 1998-07-30 2004-09-07 Solexa Ltd. Arrayed biomolecules and their use in sequencing
US20100130368A1 (en) * 1998-07-30 2010-05-27 Shankar Balasubramanian Method and system for sequencing polynucleotides
US6546883B1 (en) * 2000-07-14 2003-04-15 Rgf, Inc. Thermo-oxidizer evaporator
US7160566B2 (en) * 2003-02-07 2007-01-09 Boc, Inc. Food surface sanitation tunnel
DE102004026646B4 (de) * 2004-06-01 2007-12-13 Applikations- Und Technikzentrum Für Energieverfahrens-, Umwelt- Und Strömungstechnik (Atz-Evus) Verfahren zur thermischen Entsorgung schadstoffhaltiger Substanzen
US8113491B2 (en) 2005-02-14 2012-02-14 Neumann Systems Group, Inc. Gas-liquid contactor apparatus and nozzle plate
US8864876B2 (en) * 2005-02-14 2014-10-21 Neumann Systems Group, Inc. Indirect and direct method of sequestering contaminates
US7866638B2 (en) * 2005-02-14 2011-01-11 Neumann Systems Group, Inc. Gas liquid contactor and effluent cleaning system and method
US8398059B2 (en) 2005-02-14 2013-03-19 Neumann Systems Group, Inc. Gas liquid contactor and method thereof
US7379487B2 (en) 2005-02-14 2008-05-27 Neumann Information Systems, Inc. Two phase reactor
FI121990B (fi) * 2007-12-20 2011-07-15 Beneq Oy Laite sumun ja hiukkasten tuottamiseksi
CN107120665A (zh) * 2017-07-04 2017-09-01 大连海伊特重工股份有限公司 一种含盐废液处理装置及方法
CN107559822B (zh) * 2017-09-21 2020-06-09 哈尔滨工业大学 中心给粉旋流煤粉燃器和燃尽风布置结构
CN107559823B (zh) * 2017-09-21 2019-04-30 哈尔滨工业大学 一种炉内脱硝与两级燃尽风布置的低氮燃烧装置
CN107606602B (zh) * 2017-09-21 2019-04-16 哈尔滨工业大学 一种sncr和ofa交错布置的卧式锅炉

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Also Published As

Publication number Publication date
US5634413A (en) 1997-06-03
EP0710799A2 (fr) 1996-05-08
CA2162080A1 (fr) 1996-05-08
DE4439670A1 (de) 1996-05-09
JPH08210619A (ja) 1996-08-20
DE59509056D1 (de) 2001-04-05
EP0710799A3 (fr) 1998-01-14

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